CN107866272A - Prepare the catalyst of cyclohexyl benzene - Google Patents
Prepare the catalyst of cyclohexyl benzene Download PDFInfo
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- CN107866272A CN107866272A CN201610853125.8A CN201610853125A CN107866272A CN 107866272 A CN107866272 A CN 107866272A CN 201610853125 A CN201610853125 A CN 201610853125A CN 107866272 A CN107866272 A CN 107866272A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
- B01J29/74—Noble metals
- B01J29/7415—Zeolite Beta
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/74—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition with simultaneous hydrogenation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
- B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
- C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
- C07C2529/74—Noble metals
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Abstract
The present invention relates to the method for catalyst for preparing cyclohexyl benzene and preparation method thereof and benzene hydrogenation alkylation one-step synthesis method cyclohexyl benzene, mainly solves catalyst of the prior art and causes by-product cyclic hexane high income and the low technical problem of principal product cyclohexyl benzene yield in reaction.The present invention is by using the catalyst for preparing cyclohexyl benzene, including carrier and following active component：(1) 0.5~20g/L Pd；At least one of (2) 0~50g/L lanthanide series, wherein described carrier achieves preferable effect for the technical scheme of h-type zeolite molecular sieve, cyclohexyl benzene is prepared available for benzene hydrogenation alkylation one-step method.
Description
Technical field
The present invention relates to a kind of catalyst, its preparation method and benzene hydrogenation alkylation one-step method for preparing cyclohexyl benzene to close
Into the method for cyclohexyl benzene.
Background technology
Cyclohexyl benzene is a kind of important intermediate, is widely used in the fields such as liquid crystal, plastics, coating, adhesive.Hexamethylene
Base benzene class liquid crystal has the characteristics that high chemical stability, photochemical stability, viscosity is low and good physical properties, is aobvious
Show one of ideal material of device.Additive of the cyclohexyl benzene as lithium-ion battery electrolytes, there is anti-overcharge performance, can carry
The security performance of high battery.In addition, phenol and cyclohexanone can be prepared by the peroxidating of cyclohexyl benzene, decomposition reaction process,
For producing large industrial chemicals such as phenolic resin, caprolactam and nylon, have a good application prospect.The base of cyclohexyl benzene
This information is as follows：Colourless liquid, No. CAS is 827-52-1, molecular weight C12H16, density 0.95g/cm3, boiling point 238~240
DEG C, 5 DEG C of fusing point, 98 DEG C of flash-point.
The preparation method of cyclohexyl benzene has：Biphenyl selects hydrogenation method, alkylation process, the benzene hydrogenation alkylation of benzene and cyclohexene
Method.Wherein, benzene hydrogenation alkylation prepares the reaction principle of cyclohexyl benzene as follows (formula 1)：The reaction machine being alkylated according to benzene hydrogenation
Reason, benzene occur hydrogenation reaction, can selectively produce cyclohexene, while generating portion hexamethylene and hexamethylene two in the heart in a metal
Alkene；On acid centre with benzene alkylated reaction occurs for cyclohexene and cyclohexadiene, generates principal product cyclohexyl benzene.Therefore, adopt
Benzene hydrogenation alkylation production cyclohexyl benzene can be realized with the bicomponent catalyst with hydrogenating function and alkylation function.
The research that benzene hydrogenation alkylation prepares cyclohexyl benzene starts from the seventies and eighties in 20th century earliest.The catalysis of early development
There is the problem of cyclohexyl benzene is selectively relatively low in agent, load is developed as ExxonMobil companies are based on MCM-22 Series Molecules sieve
The catalyst (US2011/0015457A1, US2011/0021841A1) of hydrogenation metal, hexamethylene is prepared for benzene hydrogenation alkylation
Base benzene, this technology are high to the selectivity of by-product cyclic hexane.The patent US4094918 of Phillips oil companies of the U.S.,
US4219689 and US4329531, using the zeolite catalyst through Ni- RE-treateds, and using Pd as auxiliary agent, the conversion ratio of benzene and
CHB yield is all than relatively low.High income and the production of by-product cyclic hexane during cyclohexyl benzene is prepared be present in the above method
The yield of thing cyclohexyl benzene than it is relatively low the problem of.
The content of the invention
One of technical problems to be solved by the invention are the high income and main product of by-product cyclic hexane of the prior art
The problem of yield of thing cyclohexyl benzene is low, there is provided a kind of catalyst for preparing cyclohexyl benzene, use it for benzene and hydrogen reaction is closed
The advantages of having hexamethylene yield low during into cyclohexyl benzene with cyclohexyl benzene high income.
The two of the technical problems to be solved by the invention are the preparation methods of one of above-mentioned technical problem catalyst.
The three of the technical problems to be solved by the invention are the cyclohexyl using one of the above-mentioned technical problem catalyst
The synthetic method of benzene.
It is as follows to solve one of above-mentioned technical problem technical scheme：The catalyst of cyclohexyl benzene is prepared, including
Carrier and following active component：
(1) 0.5~20g/L Pd；
At least one of (2) 0~50g/L lanthanide series；
Wherein described carrier is h-type zeolite molecular sieve.
In above-mentioned technical proposal, described lanthanide series preferred La or Sm, but preferably include La and Sm simultaneously.La and Sm exist
There is synergy in terms of improving CHB yields.
In above-mentioned technical proposal, Pd contents are preferably 1~10g/L.
In above-mentioned technical proposal, zeolite molecular sieve preferably is selected from BEA, MOR or MWW zeolite molecular sieve；Preferred zeolite point
Son sieve carrier is BEA zeolite molecular sieves.
In above-mentioned technical proposal, the BEA zeolite molecular sieves are preferably binder free shaping BEA zeolite molecular sieves.It is described
The mol ratio of the silica/alumina of binder free shaping BEA zeolite molecular sieves is preferably 10~100, more preferably 20~
60。
In above-mentioned technical proposal, lanthanide content is preferably greater than 0 and is less than or equal to 50g/L, more preferably 0.1~20g/
L。
To solve the two of above-mentioned technical problem, technical scheme is as follows：The technical side of one of above-mentioned technical problem
The preparation method of catalyst described in case, is comprised the steps of：
A) the h-type zeolite molecular sieve is obtained；
B) by aequum Pd compound wiring solution-forming I；Optional compound is such as, but not limited to palladium bichloride, palladium nitrate,
At least one of ammonium chloropalladate and ammonium chloropalladite, the optional water of solvent that the solution uses and by hydrochloric acid or nitric acid or acetic acid
It is 2.0~6.5 to be tuned into pH, and for ease of year-on-year, embodiment and comparative example in the specific embodiment of the invention are with 1mol/L's
Aqueous acetic acid is solvent；
C) by the compound wiring solution-forming II of aequum lanthanide series；
D) solution II that the step b) solution Is prepared and step c) are prepared is carried on described in step a) using infusion process
On zeolite molecular sieve carrier, dry, 350~550 DEG C are calcined 3~6 hours, and catalyst is made.
In above-mentioned technical proposal, the step b) the Pd preferred palladium bichloride of compound.
In above-mentioned technical proposal, the compound preferably nitrate of the step c) lanthanide series.
In above-mentioned technical proposal, step d) impregnating process be able to can be reached using any one of following three kinds
The purpose of the present invention：
Method 1, first dipping solution I, drying, roasting, then dipping solution II again, is dried, roasting.The dipping method is having
Step impregnation I is referred to as in the table 1 of body embodiment.
Method 2, first dipping solution II, drying, roasting, then dipping solution I, dry, roasting.The dipping method is specific real
Apply and step impregnation II is referred to as in the table 1 of mode.
Method 3, impregnate, dry together after solution I and solution II are mixed, being calcined.The dipping method is in specific embodiment party
Referred to as it is mixed with dipping in the table 1 of formula.
But it has surprisingly been found that the best way is method 2, now CHB yields are higher.
It is as follows to solve three technical schemes of above-mentioned technical problem：The synthetic method of cyclohexyl benzene, with benzene and
Hydrogen is reaction raw materials, make reaction raw materials contacted with catalyst any one of the technical scheme of one of above-mentioned technical problem into
Row benzene hydrogenation alkylated reaction generates cyclohexyl benzene.
In above-mentioned technical proposal, the temperature of reaction is preferably 100~200 DEG C, more preferably 120~180 DEG C.
In above-mentioned technical proposal, in reaction raw materials the mol ratio of benzene and hydrogen be preferably 0.5~2.0, more preferably 0.5~
1.3。
In above-mentioned technical proposal, the pressure of reaction is preferably 0.5~5.0MPa (gauge pressure), more preferably 0.5~4.0MPa
(gauge pressure).
In above-mentioned technical proposal, the liquid volume of reaction raw materials benzene is preferably 0.2~3h-1, more preferably 0.2~1.5h-1。
The catalyst of the present invention is active constituent due to employing Pd and lanthanide series simultaneously, reduces by-product cyclic hexane
Yield, in lanthanide series simultaneously including in the case of La and Sm, also significantly improving target product CHB yield.Reacting
150 DEG C of temperature, benzene and hydrogen mol ratio 0.8, pressure 2.0MPa, the mass space velocity 0.5h of benzene-1Under conditions of, the yield of hexamethylene
Up to less than 5.0%, cyclohexyl benzene high income achieves preferable technique effect up to 32%.
Embodiment
【Embodiment 1】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 1.0g2It is dissolved in 1mol/L aqueous acetic acids and is made into 80g solution Is；It is a diameter of to measure 0.1L
1mm, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30)；Will
Solution I is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, is prepared into
To required catalyst.
2nd, evaluating catalyst
10ml Catalyst packings are taken to carry out activity rating after reduction activation into fixed bed reactors, condition is as follows：Reaction
Temperature be 150 DEG C, in reaction raw materials the mol ratio of benzene and hydrogen be 0.8, the pressure of reaction is 2.0MPa (gauge pressure), reaction
The liquid volume air speed of benzene feedstock is 0.5h-1。
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Comparative example 1】
1st, catalyst preparation
Weigh the La (NO of the La containing 1.0g3)3·6H2O is soluble in water to be made into 80g solution IIs；Measure a diameter of 1mm of 0.1L,
Length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30), by solution
II is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, institute is prepared
The catalyst needed.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Comparative example 2】
1st, catalyst preparation
Weigh the Sm (NO of the Sm containing 1.0g3)3·6H2O is soluble in water to be made into 80g solution IIs；Measure a diameter of 1mm of 0.1L,
Length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30), by solution
II is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, institute is prepared
The catalyst needed.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 2】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.7g
La (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then solution I and solution II are well mixed；Measure 0.1L diameters
For 1mm, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30),
Mixed solution is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, made
It is standby to obtain required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 3】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh Sm containing 0.7g
Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then solution I and solution II are well mixed；Measure 0.1L diameters
For 1mm, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30)；
Mixed solution is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, made
It is standby to obtain required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 4】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.5g
La (NO3)2·6H2The O and Sm containing 0.2g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and
Solution II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (two
30) mol ratio of silica/alumina is；Mixed solution is loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h,
100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 5】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.4g
La (NO3)3·6H2The O and Sm containing 0.3g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and
Solution II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (two
The mol ratio of silica/alumina is 30), mixed solution to be loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h,
100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 6】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.3g
La (NO3)2·6H2The O and Sm containing 0.4g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and
Solution II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (two
The mol ratio of silica/alumina is 30), mixed solution to be loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h,
100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 7】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.2g
La (NO3)2·6H2The O and Sm containing 0.5g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and
Solution II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (two
The mol ratio of silica/alumina is 30), mixed solution to be loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h,
100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 8】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.1g
La (NO3)2·6H2The O and Sm containing 0.6g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and
Solution II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (two
The mol ratio of silica/alumina is 30), mixed solution to be loaded on Hydrogen BEA zeolite molecular sieves, room temperature immersion 12h,
100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
Embodiment 4~8 is with embodiment 2~3 on year-on-year basis as can be seen that La and Sm has in terms of CHB yields are improved cooperates with work
With.【Embodiment 9】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L aqueous acetic acids and is made into 80g solution Is；It is a diameter of to measure 0.1L
1mm, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieves (mol ratio of silica/alumina is 30), will
Solution I is loaded on Hydrogen BEA zeolite molecular sieves；Room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, obtain CAT1.
Weigh the La (NO of the La containing 0.1g3)2·6H2The O and Sm containing 0.6g Sm (NO3)3·6H2O is soluble in water to be made into 80g solution IIs；
CAT1 is impregnated into solution II；Room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, are prepared required urge
Agent.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 10】
1st, catalyst preparation
Weigh the La (NO of the La containing 0.1g3)2·6H2The O and Sm containing 0.6g Sm (NO3)3·6H2O is soluble in water to be made into 80g
Solution II；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieve (silica/oxygen
The mol ratio for changing aluminium is that 30), solution II is loaded on Hydrogen BEA zeolite molecular sieves；Room temperature immersion 12h, 100 DEG C of dry 12h,
450 DEG C of roasting 4h, obtain CAT2；Weigh the PdCl of the Pd containing 0.3g2It is dissolved in 1mol/L acetic acid and is made into 80g solution Is；By CAT2
It is impregnated into solution I；Room temperature immersion 12h, 100 DEG C of dry 12h, 450 DEG C of roasting 4h, that is, are prepared required catalyst.
2nd, evaluating catalyst
Evaluating catalyst method is shown in embodiment 1.
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 11】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.5g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh the La's containing 2g
La(NO3)3·6H2The O and Sm containing 1g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；Then by solution I and solution
II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieve (titanium dioxides
The mol ratio of silicon/aluminum oxide is that 30), mixed solution is loaded on Hydrogen BEA zeolite molecular sieves；Room temperature immersion 12h, 120 DEG C
12h is dried, 430 DEG C of roasting 4h, that is, required catalyst is prepared.
2nd, evaluating catalyst
In addition to following process Parameters variation, remaining is identical with the evaluating catalyst method in embodiment 1：The temperature of reaction
Spend for 100 DEG C, the mol ratio of benzene and hydrogen is 0.5 in reaction raw materials, and the pressure of reaction is 0.5MPa (gauge pressure), the raw material of reaction
Liquid volume air speed be 0.2h-1。
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
【Embodiment 12】
1st, catalyst preparation
Weigh the PdCl of the Pd containing 0.1g2It is dissolved in 1mol/L aqueous acetic acids and is made into 40g solution Is；Weigh La containing 0.3g
La (NO3)2·6H2The O and Sm containing 0.1g Sm (NO3)3·6H2O is soluble in water to be made into 40g solution IIs；By solution I and solution
II is well mixed；Measure a diameter of 1mm of 0.1L, length 5mm binder free cylinder Hydrogen BEA zeolite molecular sieve (titanium dioxides
The mol ratio of silicon/aluminum oxide is that 30), mixed solution is loaded on Hydrogen BEA zeolite molecular sieves；Room temperature immersion 12h, 80 DEG C dry
Dry 12h, 470 DEG C of roasting 4h, that is, be prepared required catalyst.
2nd, evaluating catalyst
In addition to following process Parameters variation, remaining is identical with the evaluating catalyst method in embodiment 1：The temperature of reaction
Spend for 200 DEG C, the mol ratio of benzene and hydrogen is 2.0 in reaction raw materials, and the pressure of reaction is 3.0MPa (gauge pressure), the raw material of reaction
Liquid volume air speed be 2.0h-1。
Composition for ease of comparing catalyst is listed in table 1, and evaluation result is listed in into table 2.
The catalyst of table 1 forms
The evaluating catalyst result of table 2
Note：In table 2, CH represents hexamethylene, and CHB represents cyclohexyl benzene.
Claims (10)
1. the catalyst of cyclohexyl benzene is prepared, including carrier and following active component：
(1) 0.5~20g/L Pd；
At least one of (2) 0~50g/L lanthanide series；
Wherein described carrier is h-type zeolite molecular sieve.
2. catalyst according to claim 1, it is characterised in that described Pd contents are 1~10g/L.
3. catalyst according to claim 1, it is characterised in that described zeolite molecules are boiled screened from BEA, MOR or MWW
Stone molecular sieve.
4. catalyst according to claim 3, it is characterised in that selected BEA zeolite molecular sieves are molded for binder free
BEA zeolite molecular sieves.
5. catalyst according to claim 4, it is characterised in that the two of described binder free shaping BEA zeolite molecular sieves
The mol ratio of silica/alumina is 10~100.
6. catalyst according to claim 1, it is characterised in that in described catalyst lanthanide content be 0.1~
20g/L。
7. the preparation method of catalyst described in claim 1, is comprised the steps of：
A) the h-type zeolite molecular sieve is obtained；
B) by aequum Pd compound wiring solution-forming I；
C) by the compound wiring solution-forming II of aequum lanthanide series；
D) solution II that the step b) solution Is prepared and step c) are prepared is carried on to the zeolite described in step a) using infusion process
On molecular sieve carrier, dry, 350~550 DEG C are calcined 3~6 hours, and catalyst is made.
8. the synthetic method of cyclohexyl benzene, using benzene and hydrogen as reaction raw materials, make reaction raw materials with it is any in claim 1 to 6
The item catalyst contact carries out benzene hydrogenation alkylated reaction generation cyclohexyl benzene.
9. according to the method for claim 8, it is characterized in that the temperature of reaction is 100~200 DEG C.
10. according to the method for claim 8, it is characterized in that the liquid volume air speed of reaction raw materials benzene is 0.2~3h-1。
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| CN201610853125.8A CN107866272B (en) | 2016-09-26 | 2016-09-26 | Prepare the catalyst of cyclohexyl benzene |
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| CN201610853125.8A CN107866272B (en) | 2016-09-26 | 2016-09-26 | Prepare the catalyst of cyclohexyl benzene |
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| CN107866272A true CN107866272A (en) | 2018-04-03 |
| CN107866272B CN107866272B (en) | 2019-11-08 |
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| CN201610853125.8A Active CN107866272B (en) | 2016-09-26 | 2016-09-26 | Prepare the catalyst of cyclohexyl benzene |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102333747A (en) * | 2009-02-26 | 2012-01-25 | 埃克森美孚化学专利公司 | Process for producing cyclohexylbenzene |
| CN102844115A (en) * | 2010-06-10 | 2012-12-26 | 宇部兴产株式会社 | Catalyst for alkylation and process for producing alkylaromatic hydrocarbon compound using the catalyst |
| CN103619788A (en) * | 2011-05-18 | 2014-03-05 | 宇部兴产株式会社 | 3,3',4,4'-tetraalkyl cyclohexylbenzene and method for producing same |
| CN105233861A (en) * | 2014-07-11 | 2016-01-13 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst and synthetic method thereof |
| CN105582990A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Catalyst for producing cyclohexylbenzene |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102333747A (en) * | 2009-02-26 | 2012-01-25 | 埃克森美孚化学专利公司 | Process for producing cyclohexylbenzene |
| CN102844115A (en) * | 2010-06-10 | 2012-12-26 | 宇部兴产株式会社 | Catalyst for alkylation and process for producing alkylaromatic hydrocarbon compound using the catalyst |
| CN103619788A (en) * | 2011-05-18 | 2014-03-05 | 宇部兴产株式会社 | 3,3',4,4'-tetraalkyl cyclohexylbenzene and method for producing same |
| CN105233861A (en) * | 2014-07-11 | 2016-01-13 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst and synthetic method thereof |
| CN105582990A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Catalyst for producing cyclohexylbenzene |
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